US20010021362A1 - Method for controlling absorbent at decarboxylation facility and system therefor - Google Patents
Method for controlling absorbent at decarboxylation facility and system therefor Download PDFInfo
- Publication number
- US20010021362A1 US20010021362A1 US09/801,814 US80181401A US2001021362A1 US 20010021362 A1 US20010021362 A1 US 20010021362A1 US 80181401 A US80181401 A US 80181401A US 2001021362 A1 US2001021362 A1 US 2001021362A1
- Authority
- US
- United States
- Prior art keywords
- absorption tower
- tower
- liquid level
- controller
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000002250 absorbent Substances 0.000 title claims abstract description 43
- 230000002745 absorbent Effects 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims description 38
- 238000006114 decarboxylation reaction Methods 0.000 title claims description 26
- 238000010521 absorption reaction Methods 0.000 claims abstract description 89
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 79
- 239000007788 liquid Substances 0.000 claims abstract description 74
- 150000001412 amines Chemical class 0.000 claims abstract description 66
- 238000001816 cooling Methods 0.000 claims abstract description 19
- 238000005406 washing Methods 0.000 claims abstract description 19
- 230000001105 regulatory effect Effects 0.000 claims abstract description 15
- 230000001276 controlling effect Effects 0.000 claims description 29
- 230000008929 regeneration Effects 0.000 claims description 21
- 238000011069 regeneration method Methods 0.000 claims description 21
- 238000011084 recovery Methods 0.000 claims description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 41
- 239000007789 gas Substances 0.000 description 32
- 229910002092 carbon dioxide Inorganic materials 0.000 description 19
- 239000001569 carbon dioxide Substances 0.000 description 18
- 239000000243 solution Substances 0.000 description 16
- 230000007423 decrease Effects 0.000 description 13
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 9
- 230000003247 decreasing effect Effects 0.000 description 9
- 230000009471 action Effects 0.000 description 7
- 239000003546 flue gas Substances 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000001476 alcoholic effect Effects 0.000 description 3
- -1 amine compound Chemical class 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- OPKOKAMJFNKNAS-UHFFFAOYSA-N N-methylethanolamine Chemical compound CNCCO OPKOKAMJFNKNAS-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229920000768 polyamine Polymers 0.000 description 2
- IMNIMPAHZVJRPE-UHFFFAOYSA-N triethylenediamine Chemical compound C1CN2CCN1CC2 IMNIMPAHZVJRPE-UHFFFAOYSA-N 0.000 description 2
- XBTRYWRVOBZSGM-UHFFFAOYSA-N (4-methylphenyl)methanediamine Chemical compound CC1=CC=C(C(N)N)C=C1 XBTRYWRVOBZSGM-UHFFFAOYSA-N 0.000 description 1
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- 229940058020 2-amino-2-methyl-1-propanol Drugs 0.000 description 1
- RPNUMPOLZDHAAY-UHFFFAOYSA-N Diethylenetriamine Chemical compound NCCNCCN RPNUMPOLZDHAAY-UHFFFAOYSA-N 0.000 description 1
- PIICEJLVQHRZGT-UHFFFAOYSA-N Ethylenediamine Chemical compound NCCN PIICEJLVQHRZGT-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000002202 Polyethylene glycol Substances 0.000 description 1
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 description 1
- 239000003655 absorption accelerator Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- CBTVGIZVANVGBH-UHFFFAOYSA-N aminomethyl propanol Chemical compound CC(C)(N)CO CBTVGIZVANVGBH-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 150000007514 bases Chemical class 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 229940116318 copper carbonate Drugs 0.000 description 1
- GEZOTWYUIKXWOA-UHFFFAOYSA-L copper;carbonate Chemical compound [Cu+2].[O-]C([O-])=O GEZOTWYUIKXWOA-UHFFFAOYSA-L 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- UFEJKYYYVXYMMS-UHFFFAOYSA-N methylcarbamic acid Chemical compound CNC(O)=O UFEJKYYYVXYMMS-UHFFFAOYSA-N 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 150000004885 piperazines Chemical class 0.000 description 1
- 150000003053 piperidines Chemical class 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 150000003141 primary amines Chemical class 0.000 description 1
- 150000003235 pyrrolidines Chemical class 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003335 secondary amines Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 150000003512 tertiary amines Chemical class 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1412—Controlling the absorption process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S423/00—Chemistry of inorganic compounds
- Y10S423/05—Automatic, including computer, control
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S423/00—Chemistry of inorganic compounds
- Y10S423/06—Temperature control
Definitions
- the present invention relates to a method for controlling absorbent at a decarboxylation facility and a system therefor.
- An object of the present invention is to provide a method for controlling absorbent at a decarboxylation facility, in which water balance is controlled automatically and the concentration of amine is automatically kept proper, and a system for carrying out this method.
- the present invention provides a method for controlling an absorbent at a decarboxylation facility provided with an absorption tower having an amine recovery section and a regeneration tower, wherein a temperature controller for circulating water to the washing section of the absorption tower is controlled by a controller of the liquid level of the bottom of the absorption tower to control the temperature of the circulating water, thereby the concentration of amine in the absorbent is regulated.
- the temperature controller for circulating water to the washing section of the absorption tower is generally a temperature controller, which receives a control signal sent from the controller of the liquid level of the bottom of the absorption tower and changes a temperature set value, and regulates the flow rate by controlling a control valve while detecting temperature information sent from a temperature detector.
- the present invention provides, in another embodiment, a method for controlling absorbent at a decarboxylation facility provided with an absorption tower having an amine recovery section and a regeneration tower, wherein a temperature controller for circulating water to a cooling tower for the absorption tower is controlled by a controller of the liquid level of the bottom of the absorption tower to control the temperature of the circulating water, whereby the concentration of amine in the absorbent is regulated.
- the temperature controller for circulating water to a cooling tower for the absorption tower is generally a temperature controller, which receives a control signal sent from the controller of the liquid level of the bottom of the absorption tower and changes a temperature set value, and regulates the flow rate by controlling a control valve while detecting temperature information sent from a temperature detector.
- control method using the controller of the liquid level of the bottom of the absorption tower preferably involves sample PI control. In this case, even if a delay exists in the operation result, control can be accomplished properly.
- Such a control system comprises, in another embodiment, a controller of the liquid level of the bottom of the absorption tower and a temperature controller for circulating water to a cooling tower for the absorption tower controlled by the controller of the liquid level of the bottom of the absorption tower.
- water balance is controlled automatically and the concentration of amine is automatically kept proper.
- the temperature of the circulating water in which the temperature of the circulating water is controlled, of water content in circulating amine solution, water content lost by accompanying outlet gas is controlled, by which the concentration of amine is regulated.
- the temperature of the circulating water to the cooling tower is controlled, the water content added by accompanying inlet gas, which is one factor that determines the water content in circulating amine solution, is controlled, by which the concentration of amine is regulated.
- FIG. 1 is a schematic view for explaining one embodiment of a method for controlling absorbent at a decarboxylation facility and a system therefor;
- FIG. 2 is a flowchart for explaining a flow for regulating amine concentration in the embodiment shown in FIG. 1;
- FIG. 3 is another flowchart for explaining a flow for regulating amine concentration in the embodiment shown in FIG. 1;
- FIG. 4 is control action diagrams for explaining the details of sample PI control
- FIG. 6 is a flowchart for explaining a flow for regulating amine concentration in the embodiment shown in FIG. 5;
- FIG. 7 is another flowchart for explaining a flow for regulating amine concentration in the embodiment shown in FIG. 5;
- FIG. 8 is a graph showing an operation result of the decarboxylation facility of embodiment 1 in accordance with the present invention.
- treatment gas carbon dioxide-containing gas to be subjected to decarboxylation treatment
- fuel gas combustion flue gas, and the like
- the treatment gas may contain moisture, oxygen, and Sox, NOx, COS and other acidic gases.
- the treatment gas may have an increased pressure, normal pressure, or reduced pressure, and also have a low temperature or a high temperature, having no special restriction. It is preferably combustion flue gas with the normal pressure.
- concentration of carbon dioxide in the treatment gas is 1 to 75 vol %, preferably 5 to 20 vol %.
- amine compound As an amine compound (referred simply to as amine) used in the present invention, alcoholic hydroxyl group-containing primary amines such as monoethanolamine and 2-amino-2-methyl-1-propanol, alcoholic hydroxyl group-containing secondary amines such as diethanolamine and 2-methylaminoethanol, alcoholic hydroxyl group-containing tertiary amines such as triethanolamine and N-methyldiethanolamine, polyethylene polyamines such as ethylenediamine, triethylenediamine, and diethylenetriamine, cyclic amines such as piperazines, piperidines, and pyrrolidines, polyamines such as xylenediamine, amino acids such as methyl aminocarboxylic acid, and the like, and mixtures of these compounds can be cited.
- alcoholic hydroxyl group-containing primary amines such as monoethanolamine and 2-amino-2-methyl-1-propanol
- alcoholic hydroxyl group-containing secondary amines such as diethanolamine and 2-methyla
- amines are usually used as an aqueous solution of 10 to 70 wt % at a temperature of 0 to 100° C. at the time of absorption and at a temperature of 50 to 150° C. at the time of regeneration.
- a carbon dioxide absorption accelerator or a corrosion inhibitor such as basic copper carbonate can be added, and further methanol, polyethylene glycol, sulfolane, and the like can be added as other media.
- FIG. 1 shows one specific embodiment of a method for controlling absorbent at a decarboxylation facility and a system for carrying out this method.
- treatment gas 1 is cooled to a predetermined temperature as necessary by gas-liquid contact with water in a cooling tower 2 .
- a heat exchanger 14 is an apparatus for cooling cooling water by means of heat exchange water.
- the treatment gas 1 having been cooled to the predetermined temperature is supplied to a bottom portion of a carbon dioxide absorption tower (referred simply to as an absorption tower) 3 , and goes up in the tower having a carbon dioxide absorption section 4 and an amine recovery section 5 .
- the treatment gas 1 is brought into gas-liquid contact with absorbent 31 having passed through a heat exchanger 16 so that carbon dioxide is absorbed.
- treated flue gas 33 is discharged from the tower top.
- the gas-liquid contact ratio (L/G; unit: liter/N-m 3 ) in the carbon dioxide absorption tower is 0.5 to 20, and the absorption coefficient of carbon dioxide therein is 50 to 100%.
- the carbon dioxide absorption section 4 and the amine recovery section 5 of the carbon dioxide absorption tower 3 maybe a packed column or a plate column. Also, the carbon dioxide absorption section and the amine recovery section can be provided with a liquid scattering plate at an appropriate position.
- amine recovering water 32 which is part of regeneration tower overhead condensate 37 , is supplied to decrease the quantity of amine accompanying the treated flue gas 33 discharged from the carbon dioxide absorption tower 3 .
- recovered amine containing water 39 having been heat-exchanged by a heat exchanger 15 , is circulated from the lower part to the upper part of the amine recovery section 5 .
- Absorbent 34 having absorbed carbon dioxide (referred to as loaded absorbent) 34 is discharged from the bottom portion of the absorption tower 3 and supplied to a regeneration tower 9 , where it is regenerated into regenerated absorbent 35 .
- a heat exchanger 8 can be provided between the absorption tower 3 and the regeneration tower 9 so that low-temperature loaded absorbent 34 is heated by high-temperature regenerated absorbent 35 , whereby heat can be used effectively.
- the loaded absorbent 34 is supplied to an intermediate portion of the regeneration tower 9 , and carbon dioxide 36 is discharged from the tower top together with water vapor. In a portion above the intermediate portion of the regeneration tower 9 , a recovery stage is provided to restrain the accompanying of amine.
- the regeneration can be effected at normal pressure, increased pressure, or reduced pressure.
- the regeneration tower 9 is provided with a heater for heating and circulating the regenerated absorbent or a reboiler 17 .
- the reboiler 17 is heated by steam.
- Condensed and separated water (condensate 37 ) is supplied to the recovery stage of the regeneration tower 9 , and the remainder is returned to the amine recovery section 5 as the amine recovering water 32 .
- some of the condensate 37 is used as the amine recovering water 32 .
- a flow controller 56 has a function of controlling the flow rate of absorbent by controlling a control valve 57 so that the flow rate of the loaded absorbent is equal to a value corresponding to a correction signal (flow rate setting signal) generated from a liquid level controller 60 so that the liquid level in the regeneration tower is kept at a predetermined value.
- a flow controller 58 has a function of controlling the flow rate of the absorbent 31 to a predetermined value by controlling a control valve 59 .
- a temperature controller for the circulating water to the washing section of the absorption tower 3 52 is sample PI controlled by a tower bottom liquid level controller 51 , by which the concentration of amine is kept constant.
- the flow for this control will be described with reference to FIGS. 2 and 3 in addition to FIG. 1.
- the tower bottom liquid level controller 51 which receives liquid level information sent from a liquid level detector 53 , detects this state, the tower bottom liquid level controller 51 sends a control signal to the temperature controller 52 for the circulating water to the washing section of the absorption tower 3 so as to increase the temperature set value by a certain operating temperature amount.
- the temperature is increased by controlling a control valve 55 while detecting temperature information sent from a temperature detector 54 .
- the temperature of the circulating water to the washing section increases, and the temperature of the outlet gas 33 of the absorption tower 3 increases, so that the quantity of water accompanying the outlet gas increases.
- the water content in circulating amine solution decreases, and the tower bottom liquid level in the absorption tower 3 lowers, so that the concentration of amine increases.
- control carried out by raising the temperature set value by a certain operating temperature amount is accomplished by the above-described sample PI control.
- PI control is carried out for only control time (SW) at the start of a sample period (ST), and after the control time has elapsed, a manipulated variable (a temperature increased from the temperature set value, specifically the above-described operating temperature) is held (output hold).
- SW control time
- I integral control action
- PI control action proportional plus integral control action
- sample period and control time are set appropriately by a trial operation of system or other means.
- General guidelines for these values are as follows:
- the sample period (ST) is preferably longer.
- the shortest period T N of main disturbance applied to the process is shorter than ST, the disturbance cannot be controlled. Therefore, ST ⁇ T N /5 is a preferable setting.
- the method for controlling absorbent at a decarboxylation facility in accordance with the present invention is a process having a long length of dead time for which a control result (change of temperature setting) does not appear immediately on the measured value.
- a control result change of temperature setting
- the inventors made studies earnestly to attain the optimum method.
- the temperature controller 52 for the circulating water to the washing section of the absorption tower 3 can be controlled automatically by the tower bottom liquid level controller 51 only when such sample PI control is carried out.
- the tower bottom liquid level controller 51 which receives liquid level information sent from the liquid level detector 53 , detects this state, the tower bottom liquid level controller 51 sends a control signal to the temperature controller 52 for the circulating water to the washing section of the absorption tower 3 so as to decrease the temperature set value by a certain operating temperature amount.
- the temperature is decreased by controlling the control valve 55 while detecting temperature information sent from the temperature detector 54 .
- the temperature of the circulating water to the washing section decreases, and the temperature of the outlet gas of the absorption tower 3 decreases, so that the quantity of water accompanying the outlet gas decreases.
- the water content in circulating amine solution increases, and the tower bottom liquid level in the absorption tower 3 rises, so that the concentration of amine decreases.
- a temperature controller 61 for the circulating water to the cooling tower 2 is sample PI controlled by the tower bottom liquid level controller 51 , by which the concentration of amine is kept constant.
- the flow for this control will be described with reference to FIGS. 6 and 7 in addition to FIG. 5.
- the tower bottom liquid level controller 51 which receives liquid level information sent from the liquid level detector 53 , detects this state, the tower bottom liquid level controller 51 sends a control signal to the temperature controller 61 for the circulating water to the cooling tower 2 so as to decrease the temperature set value by a certain operating temperature amount.
- the temperature is decreased by controlling a control valve 63 while detecting temperature information sent from a temperature detector 62 .
- the cooling tower circulating water return temperature decreases, and the temperature of inlet gas of the absorption tower 3 decreases, so that the quantity of water accompanying the inlet gas decreases.
- the water content in circulating amine solution decreases, and the tower bottom liquid level in the absorption tower 3 lowers, so that the concentration of amine increases.
- the method in accordance with the embodiment shown in FIG. 5 is also a process having a long length of dead time for which a control result (change of temperature setting) does not appear immediately on the measured value.
- a control result change of temperature setting
- the inventors made studies earnestly to attain the optimum method.
- the temperature of the circulating water to the cooling tower can be controlled automatically by the tower bottom liquid level controller 51 only when such sample PI control is carried out.
- control carried out by rising the temperature set value by a certain operating temperature amount is accomplished by the above-described sample PI control.
- the principle of this control is similar to the principle already described with reference to FIG. 4.
- liquid level detecting means such as the liquid level detector 53 used in the above-described embodiments
- a differential pressure type, buoyancy type, capacitance type, ultrasonic type, and other types well known to a person skilled in the art can be used.
- a control test of absorbent at a decarboxylation facility was conducted by carrying out the sample PI control under the following conditions by using a system in accordance with the embodiment shown in FIG. 1.
Abstract
Description
- 1. Field of the Invention
- The present invention relates to a method for controlling absorbent at a decarboxylation facility and a system therefor.
- In recent years, at thermal electric power plants and boiler plants, a large amount of coal, heavy oil, or superheavy oil has been used as a fuel, so that the control of the quantity and concentration of discharged sulfur oxides mainly consisting of sulfur dioxide, nitrogen oxides, carbon dioxide, and the like has posed a problem from the viewpoint of prevention of air pollution and cleanness of global environment. Also, for carbon dioxide, together with flon gas and methane gas, the control of its discharge has been studied form the viewpoint of global warming. Therefore, methods such as a PSA (Pressure Swing Adsorption) method, a membrane separation concentration method, and a reaction absorption method using a basic compound have been studied. U.S. Pat. No. 5,318,758 has disclosed a method for effecting decarboxylation with an amine compound (hereinafter referred simply to as amine) being used as an absorbent. In this method, if the balance between the quantity of water in combustion flue gas flowing into a decarboxylation facility and the quantity of water in absorbent flowing out of the decarboxylation facility together with gas is lost, or amine in absorbent flows out of the decarboxylation facility, the concentration of amine in absorbent is liable to vary. The variations in amine concentration cause variations in the absorption rate of carbon dioxide and steam consumption in a regeneration tower.
- Conventionally, in order to make the amine concentration constant, water containing amine is extracted from an overhead drum of the regeneration tower, or the operator regulates the gas temperature at the inlet or outlet of an absorption tower manually to control the water balance. Therefore, the burden on the operator is heavy, and the cost of waste water treatment facility is excessive.
- An object of the present invention is to provide a method for controlling absorbent at a decarboxylation facility, in which water balance is controlled automatically and the concentration of amine is automatically kept proper, and a system for carrying out this method.
- To achieve the above object, the present invention provides a method for controlling an absorbent at a decarboxylation facility provided with an absorption tower having an amine recovery section and a regeneration tower, wherein a temperature controller for circulating water to the washing section of the absorption tower is controlled by a controller of the liquid level of the bottom of the absorption tower to control the temperature of the circulating water, thereby the concentration of amine in the absorbent is regulated.
- In the present invention, the controller of the liquid level of the bottom of the absorption tower is generally a liquid level controller, which receives liquid level information sent from a liquid level detector and sends a control signal to the temperature controller.
- The temperature controller for circulating water to the washing section of the absorption tower is generally a temperature controller, which receives a control signal sent from the controller of the liquid level of the bottom of the absorption tower and changes a temperature set value, and regulates the flow rate by controlling a control valve while detecting temperature information sent from a temperature detector.
- Also, the present invention provides, in another embodiment, a method for controlling absorbent at a decarboxylation facility provided with an absorption tower having an amine recovery section and a regeneration tower, wherein a temperature controller for circulating water to a cooling tower for the absorption tower is controlled by a controller of the liquid level of the bottom of the absorption tower to control the temperature of the circulating water, whereby the concentration of amine in the absorbent is regulated.
- The temperature controller for circulating water to a cooling tower for the absorption tower is generally a temperature controller, which receives a control signal sent from the controller of the liquid level of the bottom of the absorption tower and changes a temperature set value, and regulates the flow rate by controlling a control valve while detecting temperature information sent from a temperature detector.
- In the present invention, the control method using the controller of the liquid level of the bottom of the absorption tower preferably involves sample PI control. In this case, even if a delay exists in the operation result, control can be accomplished properly.
- Further, the present invention provides, as another aspect, a system for controlling absorbent at a decarboxylation facility provided with an absorption tower having an amine recovery section and a regeneration tower, wherein the system comprises a controller of the liquid level of the bottom of the absorption tower and temperature controller for circulating water to the washing section of the absorption tower controlled by the controller of the liquid level of the bottom of the absorption tower.
- Such a control system comprises, in another embodiment, a controller of the liquid level of the bottom of the absorption tower and a temperature controller for circulating water to a cooling tower for the absorption tower controlled by the controller of the liquid level of the bottom of the absorption tower. Such a control system comprises, in still another embodiment, a controller of the liquid level of the bottom of the absorption tower, a temperature controller for circulating water to the washing section of the absorption tower controlled by the controller of the liquid level of the bottom of the absorption tower, and a temperature controller for circulating water to a cooling tower for the absorption tower controlled by the controller of the liquid level of the bottom of the absorption tower, so that the temperature controller system for the circulating water to the washing section and the temperature controller system for the circulating water to the cooling tower are operated by being switched alternately.
- In the present invention, water balance is controlled automatically and the concentration of amine is automatically kept proper. In the embodiment, in which the temperature of the circulating water is controlled, of water content in circulating amine solution, water content lost by accompanying outlet gas is controlled, by which the concentration of amine is regulated. Also, in the embodiment in which the temperature of the circulating water to the cooling tower is controlled, the water content added by accompanying inlet gas, which is one factor that determines the water content in circulating amine solution, is controlled, by which the concentration of amine is regulated.
- Embodiments in accordance with the present invention will now be described with reference to the accompanying drawings, in which:
- FIG. 1 is a schematic view for explaining one embodiment of a method for controlling absorbent at a decarboxylation facility and a system therefor;
- FIG. 2 is a flowchart for explaining a flow for regulating amine concentration in the embodiment shown in FIG. 1;
- FIG. 3 is another flowchart for explaining a flow for regulating amine concentration in the embodiment shown in FIG. 1;
- FIG. 4 is control action diagrams for explaining the details of sample PI control;
- FIG. 5 is a schematic view for explaining another embodiment of a method for controlling absorbent at a decarboxylation facility and a system therefor;
- FIG. 6 is a flowchart for explaining a flow for regulating amine concentration in the embodiment shown in FIG. 5;
- FIG. 7 is another flowchart for explaining a flow for regulating amine concentration in the embodiment shown in FIG. 5; and
- FIG. 8 is a graph showing an operation result of the decarboxylation facility of
embodiment 1 in accordance with the present invention. - Embodiments of a method for controlling absorbent at a decarboxylation facility in accordance with the present invention and a system for carrying out this method will now be described in detail.
- In the present invention, as carbon dioxide-containing gas to be subjected to decarboxylation treatment (referred to as treatment gas), fuel gas, combustion flue gas, and the like can be cited. The treatment gas may contain moisture, oxygen, and Sox, NOx, COS and other acidic gases. The treatment gas may have an increased pressure, normal pressure, or reduced pressure, and also have a low temperature or a high temperature, having no special restriction. It is preferably combustion flue gas with the normal pressure. The concentration of carbon dioxide in the treatment gas is 1 to 75 vol %, preferably 5 to 20 vol %.
- As an amine compound (referred simply to as amine) used in the present invention, alcoholic hydroxyl group-containing primary amines such as monoethanolamine and 2-amino-2-methyl-1-propanol, alcoholic hydroxyl group-containing secondary amines such as diethanolamine and 2-methylaminoethanol, alcoholic hydroxyl group-containing tertiary amines such as triethanolamine and N-methyldiethanolamine, polyethylene polyamines such as ethylenediamine, triethylenediamine, and diethylenetriamine, cyclic amines such as piperazines, piperidines, and pyrrolidines, polyamines such as xylenediamine, amino acids such as methyl aminocarboxylic acid, and the like, and mixtures of these compounds can be cited. These amines are usually used as an aqueous solution of 10 to 70 wt % at a temperature of 0 to 100° C. at the time of absorption and at a temperature of 50 to 150° C. at the time of regeneration. To the absorbent, a carbon dioxide absorption accelerator or a corrosion inhibitor such as basic copper carbonate can be added, and further methanol, polyethylene glycol, sulfolane, and the like can be added as other media.
- Next, FIG. 1 shows one specific embodiment of a method for controlling absorbent at a decarboxylation facility and a system for carrying out this method.
- First, as shown in FIG. 1,
treatment gas 1 is cooled to a predetermined temperature as necessary by gas-liquid contact with water in acooling tower 2. Aheat exchanger 14 is an apparatus for cooling cooling water by means of heat exchange water. Thetreatment gas 1 having been cooled to the predetermined temperature is supplied to a bottom portion of a carbon dioxide absorption tower (referred simply to as an absorption tower) 3, and goes up in the tower having a carbondioxide absorption section 4 and anamine recovery section 5. Then, thetreatment gas 1 is brought into gas-liquid contact with absorbent 31 having passed through aheat exchanger 16 so that carbon dioxide is absorbed. After amine accompanying flue gas is recovered by water washing in theamine recovery section 5, treatedflue gas 33 is discharged from the tower top. The gas-liquid contact ratio (L/G; unit: liter/N-m3) in the carbon dioxide absorption tower is 0.5 to 20, and the absorption coefficient of carbon dioxide therein is 50 to 100%. The carbondioxide absorption section 4 and theamine recovery section 5 of the carbondioxide absorption tower 3 maybe a packed column or a plate column. Also, the carbon dioxide absorption section and the amine recovery section can be provided with a liquid scattering plate at an appropriate position. - To the
amine recovery section 5,amine recovering water 32, which is part of regenerationtower overhead condensate 37, is supplied to decrease the quantity of amine accompanying the treatedflue gas 33 discharged from the carbondioxide absorption tower 3. Also, recoveredamine containing water 39, having been heat-exchanged by aheat exchanger 15, is circulated from the lower part to the upper part of theamine recovery section 5. - Absorbent34 having absorbed carbon dioxide (referred to as loaded absorbent) 34 is discharged from the bottom portion of the
absorption tower 3 and supplied to aregeneration tower 9, where it is regenerated into regenerated absorbent 35. Aheat exchanger 8 can be provided between theabsorption tower 3 and theregeneration tower 9 so that low-temperature loaded absorbent 34 is heated by high-temperature regenerated absorbent 35, whereby heat can be used effectively. The loaded absorbent 34 is supplied to an intermediate portion of theregeneration tower 9, andcarbon dioxide 36 is discharged from the tower top together with water vapor. In a portion above the intermediate portion of theregeneration tower 9, a recovery stage is provided to restrain the accompanying of amine. The regeneration can be effected at normal pressure, increased pressure, or reduced pressure. As necessary, theregeneration tower 9 is provided with a heater for heating and circulating the regenerated absorbent or areboiler 17. Thereboiler 17 is heated by steam. For thecarbon oxide 36 and water vapor, which have been discharged from the top of theregeneration tower 9, water is condensed in acondenser 10, and the water is separated in aseparator 11, by which high-purity carbon dioxide 38 is discharged to the outside of the system. Condensed and separated water (condensate 37) is supplied to the recovery stage of theregeneration tower 9, and the remainder is returned to theamine recovery section 5 as theamine recovering water 32. As described above, some of thecondensate 37 is used as theamine recovering water 32. - A
flow controller 56 has a function of controlling the flow rate of absorbent by controlling acontrol valve 57 so that the flow rate of the loaded absorbent is equal to a value corresponding to a correction signal (flow rate setting signal) generated from aliquid level controller 60 so that the liquid level in the regeneration tower is kept at a predetermined value. Also, aflow controller 58 has a function of controlling the flow rate of the absorbent 31 to a predetermined value by controlling acontrol valve 59. - The following is a description of a control method for keeping the concentration of amine solution constant in the embodiment shown in FIG. 1.
- In this embodiment, a temperature controller for the circulating water to the washing section of the
absorption tower 3 52 is sample PI controlled by a tower bottomliquid level controller 51, by which the concentration of amine is kept constant. The flow for this control will be described with reference to FIGS. 2 and 3 in addition to FIG. 1. - First, a case where the tower bottom liquid level in the
absorption tower 3 is high is assumed. In this case, the concentration of amine solution is low. The causes for this are increased water content in inlet gas of theabsorption tower 3, decreased water content in outlet gas of theabsorption tower 3, and entrance of water into amine solution system from the outside (FIG. 2). - As shown in FIG. 2, if the tower bottom
liquid level controller 51, which receives liquid level information sent from aliquid level detector 53, detects this state, the tower bottomliquid level controller 51 sends a control signal to thetemperature controller 52 for the circulating water to the washing section of theabsorption tower 3 so as to increase the temperature set value by a certain operating temperature amount. At this time, the temperature is increased by controlling acontrol valve 55 while detecting temperature information sent from atemperature detector 54. Thereupon, the temperature of the circulating water to the washing section increases, and the temperature of theoutlet gas 33 of theabsorption tower 3 increases, so that the quantity of water accompanying the outlet gas increases. Also, the water content in circulating amine solution decreases, and the tower bottom liquid level in theabsorption tower 3 lowers, so that the concentration of amine increases. - This state is judged in the last part of the flow shown in FIG. 2. If the liquid level is still high, the temperature set value is further increased by a certain operating temperature amount. If the liquid level is normal, the state is maintained. Thus, the normal operating state is maintained.
- As described above, in this embodiment, the control carried out by raising the temperature set value by a certain operating temperature amount is accomplished by the above-described sample PI control.
- The method for the sample PI control is described with reference to the control action diagram shown in FIG. 4. PI control is carried out for only control time (SW) at the start of a sample period (ST), and after the control time has elapsed, a manipulated variable (a temperature increased from the temperature set value, specifically the above-described operating temperature) is held (output hold). In other words, control operation is performed only for a short period of time of every sample period. Here, character P denotes proportional control action and I denotes integral control action, and by these actions, proportional plus integral control action (PI control action) is regulated.
- The sample period and control time are set appropriately by a trial operation of system or other means. General guidelines for these values are as follows:
- ST=(L+T0)×(2 to 3)
- SW=ST/10
- L: dead time
- T0: delay time constant
- From the viewpoint of rise characteristics for decreasing overshoot, the sample period (ST) is preferably longer. However, when the shortest period TN of main disturbance applied to the process is shorter than ST, the disturbance cannot be controlled. Therefore, ST≦TN/5 is a preferable setting.
- The method for controlling absorbent at a decarboxylation facility in accordance with the present invention is a process having a long length of dead time for which a control result (change of temperature setting) does not appear immediately on the measured value. Thereupon, the inventors made studies earnestly to attain the optimum method. As a result, we found that the
temperature controller 52 for the circulating water to the washing section of theabsorption tower 3 can be controlled automatically by the tower bottomliquid level controller 51 only when such sample PI control is carried out. - Next, a case where the tower bottom liquid level in the
absorption tower 3 is low is assumed. In this case, the concentration of amine solution is high. The causes for this are decreased water content in inlet gas of theabsorption tower 3 and increased water content in outlet gas of the absorption tower 3 (FIG. 3). - As shown in FIG. 3, if the tower bottom
liquid level controller 51, which receives liquid level information sent from theliquid level detector 53, detects this state, the tower bottomliquid level controller 51 sends a control signal to thetemperature controller 52 for the circulating water to the washing section of theabsorption tower 3 so as to decrease the temperature set value by a certain operating temperature amount. At this time, the temperature is decreased by controlling thecontrol valve 55 while detecting temperature information sent from thetemperature detector 54. Thereupon, the temperature of the circulating water to the washing section decreases, and the temperature of the outlet gas of theabsorption tower 3 decreases, so that the quantity of water accompanying the outlet gas decreases. Also, the water content in circulating amine solution increases, and the tower bottom liquid level in theabsorption tower 3 rises, so that the concentration of amine decreases. - This state is judged in the last part of the flow shown in FIG. 3. If the liquid level is still low, the temperature set value is further decreased by a certain operating temperature amount. If the liquid level is normal, the state is maintained. Thus, the normal operating state is maintained.
- In this case as well, as described above, in this embodiment, the control carried out by lowering the temperature set value by a certain operating temperature amount is accomplished by the above-described sample PI control. The principle of this control is similar to the principle already described with reference to FIG. 4.
- FIG. 5 shows another specific embodiment of a method for controlling absorbent at a decarboxylation facility and a system for carrying out this method. In this embodiment, the elements to which the same reference numeral as that in FIG. 1 is applied have the same configuration and function as those of the elements shown in FIG. 1. Therefore, the explanation of each of the elements is omitted, and a control method for keeping the concentration of amine solution constant in the embodiment shown in FIG. 2 will be described.
- In this embodiment, a
temperature controller 61 for the circulating water to thecooling tower 2 is sample PI controlled by the tower bottomliquid level controller 51, by which the concentration of amine is kept constant. The flow for this control will be described with reference to FIGS. 6 and 7 in addition to FIG. 5. - First, a case where the tower bottom liquid level in the
absorption tower 3 is high is assumed. In this case, the concentration of amine solution is low. The causes for this are increased water content in inlet gas of theabsorption tower 3, decreased water content in outlet gas of theabsorption tower 3, and entrance of water into amine solution system from the outside (FIG. 6). - As shown in FIG. 6, if the tower bottom
liquid level controller 51, which receives liquid level information sent from theliquid level detector 53, detects this state, the tower bottomliquid level controller 51 sends a control signal to thetemperature controller 61 for the circulating water to thecooling tower 2 so as to decrease the temperature set value by a certain operating temperature amount. At this time, the temperature is decreased by controlling acontrol valve 63 while detecting temperature information sent from atemperature detector 62. Thereupon, the cooling tower circulating water return temperature decreases, and the temperature of inlet gas of theabsorption tower 3 decreases, so that the quantity of water accompanying the inlet gas decreases. Also, the water content in circulating amine solution decreases, and the tower bottom liquid level in theabsorption tower 3 lowers, so that the concentration of amine increases. - This state is judged in the last part of the flow shown in FIG. 6. If the liquid level is still high, the temperature set value is further decreased by a certain operating temperature amount. If the liquid level is normal, the state is maintained. Thus, the normal operating state is maintained.
- In this case, as described above, in this embodiment, the control carried out by lowering the temperature set value by a certain operating temperature amount is accomplished by the above-described sample PI control. The method for this control is completely the same as that in the embodiment shown in FIG. 1 that has been described with reference to FIG. 4.
- The method in accordance with the embodiment shown in FIG. 5 is also a process having a long length of dead time for which a control result (change of temperature setting) does not appear immediately on the measured value. Thereupon, the inventors made studies earnestly to attain the optimum method. As a result, we found that the temperature of the circulating water to the cooling tower can be controlled automatically by the tower bottom
liquid level controller 51 only when such sample PI control is carried out. - Next, a case where the tower bottom liquid level in the
absorption tower 3 is low is assumed. In this case, the concentration of amine solution is high. The causes for this are decreased water content in inlet gas of theabsorption tower 3 and increased water content in outlet gas of the absorption tower 3 (FIG. 7). - As shown in FIG. 7, if the tower bottom
liquid level controller 51, which receives liquid level information sent from theliquid level detector 53, detects this state, the tower bottomliquid level controller 51 sends a control signal to thetemperature controller 61 for the circulating water to thecooling tower 2 so as to increase the temperature set value by a certain operating temperature amount. At this time, the temperature is increased by controlling thecontrol valve 55 while detecting temperature information sent from thetemperature detector 54. Thereupon, the absorption tower circulating water return temperature increases, and the temperature of inlet gas of theabsorption tower 3 increases, so that the quantity of water accompanying the inlet gas increases. Also, the water content in circulating amine solution increases, and the tower bottom liquid level in theabsorption tower 3 rises, so that the concentration of amine decreases. - This state is judged in the last part of the flow shown in FIG. 7. If the liquid level is still low, the temperature set value is further increased by a certain operating temperature amount. If the liquid level is normal, the state is maintained. Thus, the normal operating state is maintained.
- In this case as well, as described above, in this embodiment, the control carried out by rising the temperature set value by a certain operating temperature amount is accomplished by the above-described sample PI control. The principle of this control is similar to the principle already described with reference to FIG. 4.
- The method for controlling absorbent at a decarboxylation facility in accordance with the present invention and the system for carrying out this method are not limited to the above-described embodiments, and all modifications, changes, and additions in a scope obvious to a person skilled in the art are embraced in the technical scope of the present invention.
- In the embodiment described with reference to FIG. 1, the temperature controller for the circulating water to the washing section of the
absorption tower 3 is sample PI controlled by the tower bottomliquid level controller 51 to keep the concentration of amine constant. Also, in the embodiment described with reference to FIG. 5, the temperature controller for the circulating water to thecooling tower 2 is sample PI controlled by the tower bottomliquid level controller 51 to keep the concentration of amine constant. The sample PI control system used in these embodiments can also be configured so as to be used for both of the embodiments. In this case, the control system has an advantage that the control system can be operated by switching to either one control system according to the operation purpose of the system for controlling absorbent. Further, in addition to the single control systems as shown in FIGS. 1 and 5, absorption tower control combining both control systems such that when one control is restricted, control is switched to the other control system is also embraced in the scope of the present invention. - As the type of the liquid level detecting means such as the
liquid level detector 53 used in the above-described embodiments, a differential pressure type, buoyancy type, capacitance type, ultrasonic type, and other types well known to a person skilled in the art can be used. - Also, as the regulating valve such as the
control valve 55 for regulating the flow rate in accordance with the control signal, a ball valve, globe valve, Venturi type valve, reseat valve, and other valves well known to a person skilled in the art can be used. - Further, as the type of the flow rate detecting means for the flow rate regulating means such as the
flow controller 56, orifice type, resistor type, fluid vibrating type, float type, vane-wheel type, electromagnetic type, ultrasonic type, and other types well known to a person skilled in the art can be used. - A control test of absorbent at a decarboxylation facility was conducted by carrying out the sample PI control under the following conditions by using a system in accordance with the embodiment shown in FIG. 1.
- Conditions
- Quantity of treatment gas: 46,000 Nm3/H
- Recovered quantity of CO2: 160 tons/day
- Absorbent: KS-1 solution (amine solution)
- Result: Automatic control operation of stable liquid level in the absorption tower was performed as shown in FIG. 8.
- The disclosure of Japanese Patent Application No.2000-065925 filed on Mar. 10, 2000 including the specification, the claims, the drawings, and the abstract is incorporated herein by reference with its entirety.
Claims (6)
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2000065925A JP4523691B2 (en) | 2000-03-10 | 2000-03-10 | Method and apparatus for controlling absorbent of decarbonation equipment |
JP2000-065925 | 2000-03-10 | ||
JP2000-65925 | 2000-03-10 |
Publications (2)
Publication Number | Publication Date |
---|---|
US20010021362A1 true US20010021362A1 (en) | 2001-09-13 |
US6579508B2 US6579508B2 (en) | 2003-06-17 |
Family
ID=18585370
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US09/801,814 Expired - Lifetime US6579508B2 (en) | 2000-03-10 | 2001-03-09 | Method for controlling absorbent at decarboxylation facility and system therefor |
Country Status (8)
Country | Link |
---|---|
US (1) | US6579508B2 (en) |
EP (1) | EP1132125B1 (en) |
JP (1) | JP4523691B2 (en) |
AU (1) | AU775772B2 (en) |
CA (1) | CA2339507C (en) |
DE (1) | DE60103571T2 (en) |
DK (1) | DK1132125T3 (en) |
RU (1) | RU2202403C2 (en) |
Cited By (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20080159937A1 (en) * | 2006-12-28 | 2008-07-03 | Ouimet Michel A | Process for the recovery of carbon dioxide from a gas stream |
US20100319540A1 (en) * | 2009-06-22 | 2010-12-23 | Basf Se | Removal of acid gases by means of an absorbent comprising a stripping aid |
US20100322842A1 (en) * | 2009-06-17 | 2010-12-23 | Mitsubishi Heavy Industries, Ltd. | Co2 recovering apparatus and method |
US20110232490A1 (en) * | 2010-03-26 | 2011-09-29 | Lei Ji | Chemical compounds for the removal of carbon dioxide from gases |
US20120282160A1 (en) * | 2009-07-23 | 2012-11-08 | Paul-Emmanuel Just | Carbon dioxide and hydrogen sulfide absorbents and process for their use |
CN102781551A (en) * | 2010-01-14 | 2012-11-14 | 阿尔斯通技术有限公司 | Water wash method and system for a carbon dioxide capture process |
EP2537575A1 (en) * | 2011-06-21 | 2012-12-26 | Kabushiki Kaisha Toshiba | Carbon dioxide capturing device and carbon dioxide capturing method |
US20130192470A1 (en) * | 2010-12-01 | 2013-08-01 | The Kansai Electric Power Co., Inc. | Co2 recovery system |
US20130333559A1 (en) * | 2011-02-28 | 2013-12-19 | Mitsubishi Heavy Industries, Ltd. | Co2 recovering apparatus and operation control method of co2 recovering apparatus |
US20140041523A1 (en) * | 2012-08-09 | 2014-02-13 | Mitsubishi Heavy Industries, Ltd. | Exhaust gas treatment system |
US10888816B2 (en) | 2016-11-01 | 2021-01-12 | Shell Oil Company | Process for producing a purified gas stream |
CN112439220A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Recovery tower kettle liquid treatment system |
GB2587046A (en) * | 2019-09-12 | 2021-03-17 | Toshiba Kk | Carbon dioxide capturing system and method of operating the same |
Families Citing this family (31)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2003033117A1 (en) | 2001-10-17 | 2003-04-24 | Mitsubishi Heavy Industries, Ltd | Flue gas desulfurization apparatus and flue gas desulfurization system, and method for operating flue gas desulfurization apparatus |
US6912859B2 (en) * | 2002-02-12 | 2005-07-05 | Air Liquide Process And Construction, Inc. | Method and apparatus for using a main air compressor to supplement a chill water system |
DE102004042656B3 (en) * | 2004-09-03 | 2005-12-29 | Draka Comteq Germany Gmbh & Co. Kg | Multi-layer, strip-shaped shielding foil for electrical lines and thus equipped electrical cable, in particular data transmission cable |
JP2006150298A (en) * | 2004-11-30 | 2006-06-15 | Mitsubishi Heavy Ind Ltd | Absorption liquid, and co2 or h2s removal apparatus and method employing it |
ATE385508T1 (en) * | 2005-02-04 | 2008-02-15 | Du Pont | COMPOSITIONS COMPRISING FLUOROCARBON GRAFTED POLYSILOXANES |
JP5021917B2 (en) * | 2005-09-01 | 2012-09-12 | 三菱重工業株式会社 | CO2 recovery apparatus and method |
DE102008035202B3 (en) * | 2008-07-28 | 2009-09-24 | Prinovis Ltd. & Co. Kg | Process for the purification of gases, in particular chemical residues |
FR2938454B1 (en) * | 2008-11-20 | 2014-08-22 | Inst Francais Du Petrole | METHOD FOR DEACIDIFYING GAS WITH AMINO-ABSORBENT SOLUTION WITH WATER-WASHING SECTION |
FR2942729B1 (en) * | 2009-03-05 | 2011-08-19 | Inst Francais Du Petrole | METHOD FOR DEACIDIFYING GAS BY ABSORBENT SOLUTION WITH OPTIMIZED WATER WASHING SECTION |
EP2408539A4 (en) * | 2009-03-18 | 2012-11-28 | Coaway Llc | Carbon dioxide removal systems |
CA2689453C (en) | 2009-06-17 | 2012-08-28 | Mitsubishi Heavy Industries, Ltd. | Co2 recovering apparatus and method |
JP5168301B2 (en) * | 2010-02-26 | 2013-03-21 | 株式会社デンソー | Exhaust purification device for internal combustion engine |
JP2011179338A (en) * | 2010-02-26 | 2011-09-15 | Denso Corp | Nox removal system for internal combustion engine |
FR2961115B1 (en) * | 2010-06-09 | 2012-06-15 | Inst Francais Du Petrole | PROCESS FOR DEACIDIFYING GAS BY ABSORBENT SOLUTION IN TWO ABSORPTION SECTIONS ARRANGED IN A COLUMN |
JP5697250B2 (en) * | 2011-06-07 | 2015-04-08 | 三菱日立パワーシステムズ株式会社 | Control method and control device for carbon dioxide removal device in combustion exhaust gas |
JP5741690B2 (en) * | 2011-07-13 | 2015-07-01 | 株式会社Ihi | Carbon dioxide recovery method and recovery apparatus |
JP5738137B2 (en) * | 2011-09-13 | 2015-06-17 | 三菱重工業株式会社 | CO2 recovery apparatus and CO2 recovery method |
JP5749677B2 (en) * | 2012-03-28 | 2015-07-15 | 株式会社東芝 | Carbon dioxide recovery system and control method thereof |
ITTV20120153A1 (en) * | 2012-08-02 | 2014-02-03 | Giorgio Eberle | ENERGY RECOVERY PLANT. |
JP6300802B2 (en) | 2012-09-05 | 2018-03-28 | ビーエーエスエフ ソシエタス・ヨーロピアBasf Se | Method for separating acid gases from fluid streams containing water |
US8486357B1 (en) * | 2012-09-12 | 2013-07-16 | Mitsubishi Heavy Industries, Ltd. | Desulfurization apparatus and method of using condensed water produced therein |
US8545782B1 (en) * | 2012-10-16 | 2013-10-01 | Mitsubishi Heavy Industries, Ltd. | CO2 recovery apparatus and CO2 recovery method |
RU2513400C1 (en) * | 2012-11-12 | 2014-04-20 | Открытое акционерное общество "Газпром" | Absorbent for removing h2s and co2 from gases |
JP6225574B2 (en) * | 2013-09-09 | 2017-11-08 | 株式会社Ihi | Carbon dioxide recovery method and recovery apparatus |
JP6248813B2 (en) * | 2014-05-28 | 2017-12-20 | 株式会社Ihi | Carbon dioxide recovery method and recovery apparatus |
JP6392091B2 (en) | 2014-11-14 | 2018-09-19 | 株式会社東芝 | Carbon dioxide recovery device and carbon dioxide recovery method |
JP6871720B2 (en) * | 2016-11-14 | 2021-05-12 | 三菱パワー株式会社 | Carbon dioxide absorber |
CN106731635A (en) * | 2017-01-20 | 2017-05-31 | 上海龙净环保科技工程有限公司 | The method and control system of control fume desulfurizing agent supply |
CA3163609A1 (en) * | 2020-01-29 | 2021-08-05 | Paul Mobley | Methods and systems for reducing the concentration of amine in wash liquid used in industrial processing |
CN112285011B (en) * | 2020-11-26 | 2022-03-01 | 中国核动力研究设计院 | High-temperature high-pressure supercritical carbon dioxide flow accelerated corrosion test system and method |
CN115400444B (en) * | 2022-08-05 | 2024-02-27 | 万华化学(宁波)有限公司 | Rectifying tower control method, storage medium and electronic equipment |
Family Cites Families (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AT350515B (en) * | 1975-08-26 | 1979-06-11 | Veitscher Magnesitwerke Ag | CONTROL SYSTEM FOR ABSORPTION COLUMNS |
GB2100471B (en) * | 1981-05-28 | 1985-03-06 | British Gas Corp | Automatic coi removal system and operation thereof |
JPS61204022A (en) * | 1985-02-12 | 1986-09-10 | Taiyo Sanso Kk | Method and apparatus for removing acid content contained in gas |
US5085839A (en) * | 1990-01-08 | 1992-02-04 | Lyondell Petrochemical Company | Apparatus for the prevention of acid gas excursions |
DE69206846T3 (en) * | 1991-03-07 | 1999-11-25 | Kansai Electric Power Co | Device and method for removing carbon dioxide from exhaust gases |
JP2539103B2 (en) * | 1991-03-07 | 1996-10-02 | 三菱重工業株式会社 | Device and method for decarbonizing flue gas |
JP3212524B2 (en) * | 1996-12-16 | 2001-09-25 | 関西電力株式会社 | Control method of flue gas decarbonation equipment |
JP3364103B2 (en) * | 1997-01-27 | 2003-01-08 | 三菱重工業株式会社 | Control method of absorption liquid in decarbonation equipment |
JP3217742B2 (en) * | 1997-11-11 | 2001-10-15 | 関西電力株式会社 | Method and apparatus for controlling carbon dioxide absorbing liquid |
US6017501A (en) * | 1997-12-26 | 2000-01-25 | Marathon Oil Company | Disposal of hydrogen sulfide gas by conversion to sulfate ions in an aqueous solution |
-
2000
- 2000-03-10 JP JP2000065925A patent/JP4523691B2/en not_active Expired - Lifetime
-
2001
- 2001-02-26 AU AU23232/01A patent/AU775772B2/en not_active Expired
- 2001-03-01 DK DK01105009T patent/DK1132125T3/en active
- 2001-03-01 EP EP01105009A patent/EP1132125B1/en not_active Expired - Lifetime
- 2001-03-01 DE DE60103571T patent/DE60103571T2/en not_active Expired - Lifetime
- 2001-03-07 RU RU2001106463/12A patent/RU2202403C2/en active
- 2001-03-07 CA CA002339507A patent/CA2339507C/en not_active Expired - Lifetime
- 2001-03-09 US US09/801,814 patent/US6579508B2/en not_active Expired - Lifetime
Cited By (22)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7601315B2 (en) * | 2006-12-28 | 2009-10-13 | Cansolv Technologies Inc. | Process for the recovery of carbon dioxide from a gas stream |
US20080159937A1 (en) * | 2006-12-28 | 2008-07-03 | Ouimet Michel A | Process for the recovery of carbon dioxide from a gas stream |
US20100322842A1 (en) * | 2009-06-17 | 2010-12-23 | Mitsubishi Heavy Industries, Ltd. | Co2 recovering apparatus and method |
US8523979B2 (en) * | 2009-06-22 | 2013-09-03 | Basf Se | Removal of acid gases by means of an absorbent comprising a stripping aid |
US20100319540A1 (en) * | 2009-06-22 | 2010-12-23 | Basf Se | Removal of acid gases by means of an absorbent comprising a stripping aid |
US20120282160A1 (en) * | 2009-07-23 | 2012-11-08 | Paul-Emmanuel Just | Carbon dioxide and hydrogen sulfide absorbents and process for their use |
CN102781551A (en) * | 2010-01-14 | 2012-11-14 | 阿尔斯通技术有限公司 | Water wash method and system for a carbon dioxide capture process |
US8795618B2 (en) * | 2010-03-26 | 2014-08-05 | Babcock & Wilcox Power Generation Group, Inc. | Chemical compounds for the removal of carbon dioxide from gases |
US20110232490A1 (en) * | 2010-03-26 | 2011-09-29 | Lei Ji | Chemical compounds for the removal of carbon dioxide from gases |
US8728220B2 (en) * | 2010-12-01 | 2014-05-20 | Mitsubishi Heavy Industries, Ltd. | CO2 recovery system |
US20130192470A1 (en) * | 2010-12-01 | 2013-08-01 | The Kansai Electric Power Co., Inc. | Co2 recovery system |
US9084959B2 (en) * | 2011-02-28 | 2015-07-21 | Mitsubishi Heavy Industries, Ltd. | CO2 recovering apparatus and operation control method of CO2 recovering apparatus |
US20130333559A1 (en) * | 2011-02-28 | 2013-12-19 | Mitsubishi Heavy Industries, Ltd. | Co2 recovering apparatus and operation control method of co2 recovering apparatus |
EP2537575A1 (en) * | 2011-06-21 | 2012-12-26 | Kabushiki Kaisha Toshiba | Carbon dioxide capturing device and carbon dioxide capturing method |
CN102836617A (en) * | 2011-06-21 | 2012-12-26 | 株式会社东芝 | Carbon dioxide capturing device and carbon dioxide capturing method |
US20120325089A1 (en) * | 2011-06-21 | 2012-12-27 | Kabushiki Kaisha Toshiba | Carbon dioxide capturing device and carbon dioxide capturing method |
US20140041523A1 (en) * | 2012-08-09 | 2014-02-13 | Mitsubishi Heavy Industries, Ltd. | Exhaust gas treatment system |
US10888816B2 (en) | 2016-11-01 | 2021-01-12 | Shell Oil Company | Process for producing a purified gas stream |
CN112439220A (en) * | 2019-09-05 | 2021-03-05 | 中石油吉林化工工程有限公司 | Recovery tower kettle liquid treatment system |
GB2587046A (en) * | 2019-09-12 | 2021-03-17 | Toshiba Kk | Carbon dioxide capturing system and method of operating the same |
GB2587046B (en) * | 2019-09-12 | 2023-01-11 | Toshiba Kk | Carbon dioxide capturing system and method of operating the same |
US11559764B2 (en) | 2019-09-12 | 2023-01-24 | Kabushiki Kaisha Toshiba | Carbon dioxide capturing system and method of operating the same |
Also Published As
Publication number | Publication date |
---|---|
DE60103571D1 (en) | 2004-07-08 |
CA2339507C (en) | 2005-07-05 |
DK1132125T3 (en) | 2004-07-12 |
DE60103571T2 (en) | 2005-06-23 |
AU775772B2 (en) | 2004-08-12 |
EP1132125A1 (en) | 2001-09-12 |
RU2202403C2 (en) | 2003-04-20 |
JP4523691B2 (en) | 2010-08-11 |
EP1132125B1 (en) | 2004-06-02 |
CA2339507A1 (en) | 2001-09-10 |
US6579508B2 (en) | 2003-06-17 |
AU2323201A (en) | 2001-09-13 |
JP2001252524A (en) | 2001-09-18 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US6579508B2 (en) | Method for controlling absorbent at decarboxylation facility and system therefor | |
JP3364103B2 (en) | Control method of absorption liquid in decarbonation equipment | |
JP4959303B2 (en) | Exhaust gas treatment method and treatment apparatus | |
EP0880990B1 (en) | Process for removing carbon dioxide from gases | |
JP3217742B2 (en) | Method and apparatus for controlling carbon dioxide absorbing liquid | |
CN100512927C (en) | Method for recovery of CO2 from gas streams | |
KR101746235B1 (en) | Energy saving method and apparatus for carbon dioxide capture in power plant | |
JP4699039B2 (en) | Exhaust gas treatment method and treatment apparatus | |
EP0558019A2 (en) | Method for removing carbon dioxide from combustion exhaust gas | |
US5085839A (en) | Apparatus for the prevention of acid gas excursions | |
EP0588175A2 (en) | Process for removing carbon dioxide from combustion gases | |
JP3212524B2 (en) | Control method of flue gas decarbonation equipment | |
EP2679295B1 (en) | Carbon dioxide recovering apparatus and method for operating the same | |
AU2010200176A1 (en) | CO2 recovering apparatus and method | |
JP2685247B2 (en) | How to remove ammonia | |
EP0671199A2 (en) | Method for the removal of carbon dioxide and sulfor oxides from combustion exhaust gas | |
AU2009245832A1 (en) | CO2 recovering apparatus and method | |
JPH0751537A (en) | Removal of co2 in co2-containing gas | |
AU2008335280B2 (en) | System and method for removal of an acidic component from a process stream | |
JP2016131917A (en) | Recovery device and recovery method of carbon dioxide | |
EP0437338A1 (en) | Apparatus for the prevention of acid excursions | |
JP2592115B2 (en) | Method for gradually removing SO lower 2 from exhaust gas containing SO 2 | |
JP2923092B2 (en) | Method for removing carbon dioxide from flue gas | |
EP0398199B1 (en) | Desulfurizing method and equipment for exhaust gas from combuster | |
KR101630054B1 (en) | System for collecting acid gas and method for collecting the same |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: MITSUBISHI HEAVY INDUSTRIES, LTD., JAPAN Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:ISHIDA, KAZUO;REEL/FRAME:012054/0094 Effective date: 20010201 |
|
STCF | Information on status: patent grant |
Free format text: PATENTED CASE |
|
FEPP | Fee payment procedure |
Free format text: PAYER NUMBER DE-ASSIGNED (ORIGINAL EVENT CODE: RMPN); ENTITY STATUS OF PATENT OWNER: LARGE ENTITY Free format text: PAYOR NUMBER ASSIGNED (ORIGINAL EVENT CODE: ASPN); ENTITY STATUS OF PATENT OWNER: LARGE ENTITY |
|
CC | Certificate of correction | ||
FPAY | Fee payment |
Year of fee payment: 4 |
|
FPAY | Fee payment |
Year of fee payment: 8 |
|
FPAY | Fee payment |
Year of fee payment: 12 |
|
AS | Assignment |
Owner name: MITSUBISHI HEAVY INDUSTRIES, LTD., JAPAN Free format text: CHANGE OF ADDRESS;ASSIGNOR:MITSUBISHI HEAVY INDUSTRIES, LTD.;REEL/FRAME:047054/0625 Effective date: 20030515 Owner name: MITSUBISHI HEAVY INDUSTRIES ENGINEERING, LTD., JAP Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:MITSUBISHI HEAVY INDUSTRIES, LTD.;REEL/FRAME:047054/0898 Effective date: 20180101 |